CN213679853U - Preparation system of liquid salt for alkali production - Google Patents
Preparation system of liquid salt for alkali production Download PDFInfo
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- CN213679853U CN213679853U CN202022615481.0U CN202022615481U CN213679853U CN 213679853 U CN213679853 U CN 213679853U CN 202022615481 U CN202022615481 U CN 202022615481U CN 213679853 U CN213679853 U CN 213679853U
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- 150000003839 salts Chemical class 0.000 title claims abstract description 218
- 239000007788 liquid Substances 0.000 title claims abstract description 144
- 239000003513 alkali Substances 0.000 title claims abstract description 17
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 16
- 238000002360 preparation method Methods 0.000 title claims abstract description 13
- 239000002699 waste material Substances 0.000 claims abstract description 39
- 238000002156 mixing Methods 0.000 claims abstract description 23
- 238000003860 storage Methods 0.000 claims abstract description 19
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 49
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims description 39
- 239000012267 brine Substances 0.000 claims description 37
- 239000013505 freshwater Substances 0.000 claims description 21
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 abstract description 19
- 239000011780 sodium chloride Substances 0.000 abstract description 10
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 abstract description 7
- 238000000034 method Methods 0.000 abstract description 7
- 238000011084 recovery Methods 0.000 abstract description 5
- 239000012535 impurity Substances 0.000 abstract description 4
- 238000000605 extraction Methods 0.000 abstract description 3
- 239000011707 mineral Substances 0.000 description 18
- 229910052500 inorganic mineral Inorganic materials 0.000 description 17
- 239000002244 precipitate Substances 0.000 description 17
- 235000010755 mineral Nutrition 0.000 description 16
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 10
- 238000011010 flushing procedure Methods 0.000 description 8
- 238000004062 sedimentation Methods 0.000 description 6
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 5
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 4
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 4
- 229910001424 calcium ion Inorganic materials 0.000 description 4
- 238000001514 detection method Methods 0.000 description 4
- 229910001425 magnesium ion Inorganic materials 0.000 description 4
- 239000013049 sediment Substances 0.000 description 4
- 235000017550 sodium carbonate Nutrition 0.000 description 4
- 229910000029 sodium carbonate Inorganic materials 0.000 description 4
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 description 3
- 239000000347 magnesium hydroxide Substances 0.000 description 3
- 229910001862 magnesium hydroxide Inorganic materials 0.000 description 3
- 239000011575 calcium Substances 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 239000012295 chemical reaction liquid Substances 0.000 description 2
- 238000005034 decoration Methods 0.000 description 2
- -1 hydroxide ions Chemical class 0.000 description 2
- 239000011777 magnesium Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000002002 slurry Substances 0.000 description 2
- 239000001110 calcium chloride Substances 0.000 description 1
- 229910001628 calcium chloride Inorganic materials 0.000 description 1
- 238000005352 clarification Methods 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
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Abstract
The utility model discloses a system is with preparation system of liquid salt to system alkali, it includes blending tank, first salt bucket, storage salt storehouse, one-level settler and first buffer tank. Has the advantages that: the liquid salt preparation system of the utility model has simple connection structure and easy realization; the utility model improves the extraction amount of sodium chloride; the utilization rate of resources is improved, and the production cost is reduced; the method has the advantages that impurities such as sulfate ions in the liquid salt are removed, the quality of the liquid salt is improved, the liquid salt is ensured to meet the standard requirements, and the use value of the liquid salt is improved; meanwhile, the recovery of useful components in the ammonia-soda waste liquid is realized, and resources are saved.
Description
The technical field is as follows:
the patent of the utility model belongs to the technical field of liquid salt production, concretely relates to preparation system of liquid salt for system alkali.
Background art:
in the industrial production of salt, the salt is called as 'industrial mother'; the salt chemical industry mainly comprises two industries of chlor-alkali and soda ash (commonly called as 'double alkali'); with the increasing demand of two alkalis for liquid salt, more and more manufacturers begin to produce and sell liquid salt for alkali production in the salt production industry, and the brine preparation process is different due to different requirements on brine indexes and different requirements of the two alkalis and the salt production industry.
At present, liquid salt is mainly produced by mixing a lean ore containing sodium chloride in a salt lake with fresh water to prepare saturated brine, and then clarifying the saturated brine to obtain liquid salt serving as a raw material to be supplied to a soda preparation working section for producing soda, and the method has the following problems:
1. the liquid salt obtained after clarification is very easy to contain a large amount of sulfate ions and other impurities, so that the liquid salt frequently does not meet the requirements of producing soda ash, the raw material liquid salt is limited, and the use value is not high;
2. the ammonia-soda waste liquor (mainly containing Ca (OH)) produced in the process of producing soda ash in the soda ash preparation section at present2、CaCl2NaCl, and water) directly as wastewater treatment, not only causes waste of resources, but also increases the cost of water treatment.
The utility model has the following contents:
the first objective of the present invention is to provide a system for preparing liquid salt for alkali production, which has a simple connection structure.
The second objective of the present invention is to provide a method for preparing liquid salt for alkali production, which can remove sulfate ions.
The technical scheme of the utility model discloses a preparation system of liquid salt for alkali production on one hand, which comprises a mixing tank, a first salt dissolving barrel, a salt storage bin, a primary settler and a first buffer tank; the liquid outlet of the ammonia-soda waste liquid pipeline and the water outlet of the fresh water pipeline are both communicated with the liquid inlet of the mixing tank; the liquid outlet of the mixing tank and the water outlet of the fresh water pipeline are both communicated with the liquid inlet of the first salt dissolving barrel; the discharge hole of the salt storage bin is connected with the feed inlet of the first salt dissolving barrel; an overflow port of the first salt tank is communicated with a liquid inlet of the primary settler; and an overflow port of the primary settler is communicated with a liquid inlet of the first cache tank.
Further, the device also comprises a second salt bucket; the liquid outlet of the mixing tank and the water outlet of the fresh water pipeline are both communicated with the liquid inlet of the second salt dissolving barrel; the discharge hole of the salt storage bin is connected with the feed inlet of the second salt dissolving barrel; and an overflow port of the second salt tank is communicated with a liquid inlet of the primary settler.
Further, the salt slurry pool is also included; overflow ports of the first salt tank and the second salt tank are communicated with a liquid inlet of the salt mud water tank; the salt mud outlets of the first salt tank and the second salt tank are communicated with the liquid inlet of the salt mud water tank; and the overflow port of the salt mud water tank is respectively communicated with the liquid inlets of the first salt dissolving tank and the second salt dissolving tank.
Further, the system also comprises a reactor, a secondary settler and a second cache tank; liquid outlets of the first cache tank and the mixing tank are communicated with a liquid inlet of the reactor; the liquid outlet of the reactor is communicated with the liquid inlet of the secondary settler; and an overflow port of the secondary settler is communicated with a liquid inlet of the second cache tank.
The utility model discloses another aspect still discloses a preparation method of liquid salt for making alkali, and it includes following step:
(1) pretreatment: mixing the ammonia-soda waste liquid and fresh water in a mixing tank according to the ratio of 1:20 to obtain diluted ammonia-soda waste liquid;
(2) salt dissolving: firstly, adding a certain amount of salt minerals into a first salt tank, then adding the diluted ammonia-soda waste liquid obtained in the step 1 into the first salt tank, and mixing and reacting with the salt minerals to obtain first brine and first precipitates, wherein calcium ions in the diluted ammonia-soda waste liquid react with sulfate ions in the salt minerals to generate calcium sulfate precipitates, and magnesium ions in the salt minerals react with hydroxide ions in the diluted ammonia-soda waste liquid to generate magnesium hydroxide precipitates;
(3) settling separation: and (3) conveying the first brine obtained in the step (2) to a first-stage settler for sedimentation to obtain standard liquid salt, and allowing the liquid salt to flow out of an overflow port of the first-stage settler to a first buffer tank for temporary storage.
Further, adding a certain amount of salt minerals into the second cleaned salt bucket; carrying out primary baume degree detection on the first brine in the step 2 at intervals of 1h, stopping conveying the first brine to the primary settler when the detected baume degree value is lower than 24 baume degrees, starting conveying the first brine to a salt mud water tank for settlement, conveying the brine overflowing from the salt mud water tank after settlement to the second salt barrel to be mixed and reacted with the salt mineral, and obtaining second brine and a second precipitate; and conveying the second brine to a first-stage settler for sedimentation to obtain standard liquid salt, and allowing the liquid salt to flow out of an overflow port of the first-stage settler to a first buffer tank for temporary storage.
Further, when the detected baume value of the first salt water is lower than 15 baume, stopping introducing the ammonia-soda waste liquid into the first salt tank, starting introducing the ammonia-soda waste liquid into the second salt tank, then sending the first salt water and the first precipitate in the first salt tank into the salt mud water tank, flushing the first salt tank with fresh water until the first salt tank is cleaned, and stopping flushing with fresh water; and regularly digging out sediments in the salt mud water tank through an excavator.
Further, a certain amount of salt minerals are added into the first cleaned salt barrel, the second brine is subjected to baume degree detection for one time at intervals of 1 hour, when the baume degree detected is lower than 24 baume degrees, the second brine is stopped being conveyed to the primary settler, the second brine starts being conveyed to the salt mud water tank for settlement, the brine overflowing from the salt mud water tank after settlement is conveyed to the first salt barrel again to be mixed and reacted with the salt minerals, and the first brine and the first precipitate are obtained.
Further, when the detected baume value of the second brine is lower than 15 baume, stopping introducing the ammonia-soda waste liquid into the second salt tank, starting introducing the ammonia-soda waste liquid into the first salt tank, then sending the second brine and the second precipitate in the second salt tank into the salt mud water tank, flushing the second salt tank with fresh water until the first salt tank is cleaned, and stopping flushing with fresh water; and regularly digging out sediments in the salt mud water tank through an excavator.
Further, when the liquid salt in the first buffer tank does not reach the standard, the liquid salt is sent into the reactor to be mixed and reacted with the ammonia-soda waste liquid again to obtain mixed brine, the mixed brine is sent into a second-stage settler to be settled to obtain standard brine and precipitates, and the standard brine flows out of an overflow port of the second-stage settler to be temporarily stored in a second buffer tank.
The utility model has the advantages that:
1. the liquid salt preparation system of the utility model has simple connection structure and easy realization; the ammonia-soda waste liquid is taken as reaction liquid to be conveyed to the system for preparing liquid salt, thereby realizing the recovery of the ammonia-soda waste liquid, avoiding the waste of resources and reducing the cost of water treatment;
2. in the utility model, the first salt tank and the second salt tank exchange salt and wash salt, thereby improving the extraction amount of sodium chloride; the utilization rate of resources is improved, and the production cost is reduced;
3. the Ca in the ammonia-soda waste liquid of the utility model2+With SO in salt minerals4 2-Calcium sulfate precipitation is generated, OH in the ammonia-soda waste liquid-With Mg in salt minerals2+Magnesium hydroxide precipitate is generated, NaCl and water in the ammonia-soda waste liquid are recycled into the liquid salt, so that impurities such as sulfate ions in the liquid salt are removed, the quality of the liquid salt is improved, the liquid salt is ensured to meet the standard requirement, and the use value of the liquid salt is improved; meanwhile, the recovery of useful components in the ammonia-soda waste liquid is realized, and resources are saved.
Description of the drawings:
fig. 1 is a schematic view of the overall structure of the embodiment of the present invention.
Mixing tank 1, first salt storage tank 2, salt storage bin 3, first-level settler 4, first buffer tank 5, second salt storage tank 6, salt mud pond 7, reactor 8, second-level settler 9, second buffer tank 10, ammonia-soda waste liquid pipeline 11, fresh water pipeline 12.
The specific implementation mode is as follows:
the present invention will be described in further detail by way of examples with reference to the accompanying drawings.
Example 1: as shown in fig. 1, a system for preparing liquid salt for alkali production includes a mixing tank 1, a first salt storage tank 2, a salt storage bin 3, a primary settler 4, a first buffer tank 5, a second salt storage tank 6, a salt mud water tank 7, a reactor 8, a secondary settler 9 and a second buffer tank 10; the liquid outlet of the ammonia-soda waste liquid pipeline 11 and the water outlet of the fresh water pipeline 12 are both communicated with the liquid inlet of the mixing tank 1; the liquid outlet of the mixing tank 1 and the water outlet of the fresh water pipeline 12 are both communicated with the liquid inlet of the first salt dissolving barrel 2; the discharge hole of the salt storage bin 3 is connected with the feed inlet of the first salt dissolving barrel 2; an overflow port of the first salt tank 2 is communicated with a liquid inlet of the primary settler 4; an overflow port of the first-stage settler 4 is communicated with a liquid inlet of the first buffer tank 5.
The liquid outlet of the mixing tank 1 and the water outlet of the fresh water pipeline 12 are both communicated with the liquid inlet of the second salt dissolving barrel 6; the discharge hole of the salt storage bin 3 is connected with the feed inlet of the second salt dissolving barrel 6; an overflow port of the second salt dissolving bucket 6 is communicated with a liquid inlet of the primary settler 4.
Overflow ports of the first salt tank 2 and the second salt tank 6 are communicated with a liquid inlet of the salt mud water tank 7; the salt mud outlets of the first salt tank 2 and the second salt tank 6 are communicated with the liquid inlet of the salt mud water tank 7; the overflow port of the salt slurry water tank 7 is respectively communicated with the liquid inlets of the first salt dissolving tank 2 and the second salt dissolving tank 6.
The liquid outlets of the first cache tank 5 and the mixing tank 1 are both communicated with the liquid inlet of the reactor 8; the liquid outlet of the reactor 8 is communicated with the liquid inlet of the secondary settler 9; an overflow port of the secondary settler 9 is communicated with a liquid inlet of the second buffer tank 10.
The liquid salt preparation system of the utility model has simple connection structure and easy realization; carry the ammonia-soda waste liquid as the reaction liquid in the system for preparing liquid salt of the utility model, realize the recovery of the ammonia-soda waste liquid, avoid the waste of resources and reduce the cost of water treatment.
Example 2: a method of preparing a liquid salt for making alkali using the system of example 1, comprising the steps of:
(1) pretreatment: mixing the ammonia-soda waste liquid and fresh water in a mixing tank 1 according to the ratio of 1:20 to obtain diluted ammonia-soda waste liquid;
(2) salt dissolving: firstly, a certain amount of salt minerals are added into a first salt tank 2, then the diluted ammonia-soda waste liquid obtained in the step 1 is added into the first salt tank 2 and is mixed and reacted with the salt minerals to obtain first brine and first precipitates, wherein calcium ions in the diluted ammonia-soda waste liquid react with sulfate ions in the salt minerals to generate calcium sulfate precipitates, magnesium ions in the salt minerals react with hydroxide ions in the diluted ammonia-soda waste liquid to generate magnesium hydroxide precipitates, NaCl and water in the ammonia-soda waste liquid are recycled into liquid salts, so that the removal of impurities such as sulfate ions in the liquid salts is realized, the quality of the liquid salts is improved, the liquid salts are ensured to meet standard requirements, and the use value of the liquid salts is improved; meanwhile, the recovery of useful components in the ammonia-soda waste liquid is realized, and resources are saved;
(3) settling separation: and (3) conveying the first brine in the step (2) to a primary settler (4) for sedimentation to obtain standard liquid salt, and allowing the liquid salt to flow out of an overflow port of the primary settler (4) to a first buffer tank (5) for temporary storage.
Adding a certain amount of salt minerals into the second cleaned salt tank 6; carrying out primary baume degree detection on the first brine in the step 2 at intervals of 1h, stopping conveying the first brine to the primary settler 4 when the detected baume degree is lower than 24 baume degrees, starting conveying the first brine to the salt mud water tank 7 for settlement, conveying the brine overflowing from the salt mud water tank 7 after settlement to a second salt barrel 6 for mixed reaction with salt minerals to obtain second brine and second precipitates; and conveying the second brine to a primary settler 4 for sedimentation to obtain standard liquid salt, and allowing the liquid salt to flow out of an overflow port of the primary settler 4 to a first buffer tank 5 for temporary storage.
When the detected baume value of the first salt water is lower than 15 baume, stopping introducing the ammonia-soda waste liquid into the first salt tank 2, starting introducing the ammonia-soda waste liquid into the second salt tank 6, then sending the first salt water and the first precipitate in the first salt tank 2 into the salt mud water tank 7, flushing the first salt tank 2 with fresh water until the first salt tank 2 is cleaned, and stopping flushing with fresh water; the sediment in the brine pond 7 is periodically dug out by an excavator.
Adding a certain amount of salt minerals into the first salt tank 2 which is cleaned up, carrying out baume degree detection on the second brine at intervals of 1h, stopping conveying the second brine to the primary settler 4 when the detected baume degree is lower than 24 baume degrees, starting conveying the second brine to the salt mud water tank 7 for sedimentation, conveying the brine overflowing from the salt mud water tank 7 after sedimentation to the first salt tank 2 for mixed reaction with the salt minerals, and obtaining first brine and first precipitates.
When the detected baume value of the second salt water is lower than 15 baume, stopping introducing the ammonia-soda waste liquid into the second salt tank 6, starting introducing the ammonia-soda waste liquid into the first salt tank 2, then sending the second salt water and the second precipitate in the second salt tank 6 into the salt mud water tank 7, flushing the second salt tank 6 with fresh water until the first salt tank 2 is cleaned, and stopping flushing with fresh water; the sediment in the brine pond 7 is periodically dug out by an excavator.
When the liquid salt in the first buffer tank 5 does not reach the standard, the liquid salt is sent into the reactor 8 to be mixed and reacted with the ammonia-soda waste liquid again to obtain mixed salt water, the mixed salt water is sent into the second-stage settler 9 to be settled to obtain standard salt water and precipitates, and the standard salt water flows out of an overflow port of the second-stage settler 9 to be temporarily stored in the second buffer tank 10.
The first salt tank 2 and the second salt tank 6 exchange salt and wash salt, so that the extraction amount of sodium chloride is increased; the utilization rate of resources is improved, and the production cost is reduced.
Example 3:
according to the prior art, when the liquid salt is 24 Baume degrees, the contents of the components are Mg2+0.6-0.8g/L, Ca2+1.2-1.4g/L of SO4 2+10-16g/L, NaCl 300-305g/L, according to the method of the embodiment 2 of the present invention, when the liquid salt is 24 Baume degrees, the content of each component is Mg2+<0.6g/L，Ca2+＜1g/L，SO4 2+Less than 10g/L, NaCl more than 305 g/L; compared with the prior art, the method of the embodiment 2 of the utility model reduces the Mg content in the liquid salt2+、SO4 2+The content of the plasma improves the content of NaCl, further improves the quality of the liquid salt, ensures that the liquid salt meets the standard requirement, and improves the use value of the liquid salt.
The above is the preferred embodiment of the present invention, and for those skilled in the art, without departing from the principle of the present invention, several improvements and decorations can be made, and these improvements and decorations should also be regarded as the protection scope of the present invention.
Claims (4)
1. A preparation system of liquid salt for alkali production is characterized by comprising a mixing tank, a first salt dissolving barrel, a salt storage bin, a first-stage settler and a first buffer tank;
the liquid outlet of the ammonia-soda waste liquid pipeline and the water outlet of the fresh water pipeline are both communicated with the liquid inlet of the mixing tank;
the liquid outlet of the mixing tank and the water outlet of the fresh water pipeline are both communicated with the liquid inlet of the first salt dissolving barrel; the discharge hole of the salt storage bin is connected with the feed inlet of the first salt dissolving barrel;
an overflow port of the first salt tank is communicated with a liquid inlet of the primary settler; and an overflow port of the primary settler is communicated with a liquid inlet of the first cache tank.
2. The system for preparing liquid salt for alkali production according to claim 1, further comprising a second salt tank;
the liquid outlet of the mixing tank and the water outlet of the fresh water pipeline are both communicated with the liquid inlet of the second salt dissolving barrel; the discharge hole of the salt storage bin is connected with the feed inlet of the second salt dissolving barrel;
and an overflow port of the second salt tank is communicated with a liquid inlet of the primary settler.
3. The system for preparing a liquid salt for making alkali according to claim 2, further comprising a brine pond;
overflow ports of the first salt tank and the second salt tank are communicated with a liquid inlet of the salt mud water tank;
the salt mud outlets of the first salt tank and the second salt tank are communicated with the liquid inlet of the salt mud water tank;
and the overflow port of the salt mud water tank is respectively communicated with the liquid inlets of the first salt dissolving tank and the second salt dissolving tank.
4. The system for preparing liquid salt for alkali production according to any one of claims 1 to 3, further comprising a reactor, a secondary settler and a second buffer tank;
liquid outlets of the first cache tank and the mixing tank are communicated with a liquid inlet of the reactor; the liquid outlet of the reactor is communicated with the liquid inlet of the secondary settler; and an overflow port of the secondary settler is communicated with a liquid inlet of the second cache tank.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113173589A (en) * | 2020-11-11 | 2021-07-27 | 内蒙古兰太钠业有限责任公司 | Preparation system and process method of liquid salt for alkali production |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113173589A (en) * | 2020-11-11 | 2021-07-27 | 内蒙古兰太钠业有限责任公司 | Preparation system and process method of liquid salt for alkali production |
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Address after: 750336 south of Ulanbuhe street, Alxa Economic Development Zone, Alxa League, Inner Mongolia Autonomous Region (WuSitai town) Patentee after: China Salt Inner Mongolia Chemical sodium Industry Co.,Ltd. Patentee after: China Salt Inner Mongolia Chemical Co.,Ltd. Address before: 750336 south of Ulanbuhe street, Alxa Economic Development Zone, Alxa League, Inner Mongolia Autonomous Region (WuSitai town) Patentee before: INNER MONGOLIA LANTAI SODIUM INDUSTRY Co.,Ltd. Patentee before: China Salt Inner Mongolia Chemical Co.,Ltd. |